Biodegradable sulfonate detergents

ABSTRACT

Novel compositions of matter which are useful as biodegradable detergents comprise alkali metal disubstituted cyclohexyl sulfonates. The compounds, as exemplified by sodium(noctylcyclohexyl)methano sulfonate, are prepared by condensing butadiene with allyl chloride, hydrogenating the ring, thereafter ring alkylating with an olefin in the presence of a free-radical generating compound and reacting the disubstituted cyclohexane with an alkali metal salt of a sulfur-containing compound to form the desired product.

United States Patent [191 Bloch [451 Nov. 11,1975

[54] BIODEGRADABLE SULFONATE DETERGENTS [75] Inventor: Herman S. Bloch, Skokie, Ill.

[73] Assignee: Universal Oil Products Company, Des Plaines. lll.

221 Filed: Dec. 4, 1974 211 Appl.No.:529,3l8

Related U.S. Application Data [63] Continuation-impart of Ser, No, 277,837. Aug. 3.

[972. Pm. NO, 3.867432.

[52] US. Cl 260/503; 252/549; 260/648 R [51] Int. Cl. C07C 143/00 [58] Field of Search 260/503 [56] References Cited UNITED STATES PATENTS 3,168,555 2/[965 Clippinger 260/503 Primary Examiner-Howard T. Mars Assistant E.\'aminerA. Siegcl Attorney, Agent. or FirmJames R. Hoatson, Jr.; Raymond H. Nelson; William H. Page, II

[ 57 ABSTRACT 6 Claims, No Drawings BIODEGRADABLE SULFONATE DETERGENTS CROSS-REFERENCE TO RELATED APPLICATIONS This application is a continuation-in-part of my copending application Ser. No. 277,837 filed Aug. 3, I972, now US. Pat. No. 3,867,432 all the teachings of which are specifically incorporated herein by reference thereto.

This invention relates to novel compositions of matter and also to a process for preparing these compounds which are useful as biodegradable detergents. More specifically, the invention is concerned with these compounds comprising alkali metal salts of disubstituted cyclohexane sulfonates which are biodegradable in nature when formed.

One of the major problems which is prevalent in population centers throughout the world is the disposal of sewage containing detergents dissolved therein. Such disposal problems are especially trying in the case of branched chained alkylaryl detergents. These detergents produce stable foams in hard or soft waters in such large quantities that the foam clogs sewage treatment facilities, and destroys the bacteria which are necessary for proper sewage treatment. In many rivers, streams, lakes, etc., which act as a water supply for the aforesaid population centers, there are found these unwanted foams and suds. As hereinbefore set forth, the presence of these unwanted foams or suds is due in many instances to the use of detergents which are nonbiodegradable in nature and which will not break down by bacterial action thereon. The non-biodegradable nature of these detergents is due to the fact that the alkyl side chain of the molecule is in many instances highly branched and therefore not readily attacked by the organisms which would ordinarily destroy the molecule. In contradistinction to this, the use of straight chain alkyl substituents on the ring will permit the detergents to be destroyed and therefore foams or suds will not build up on the surface of the water.

It is therefore an object of this invention to provide a novel method for the manufacture of biodegradable detergents which may be degraded in both urban and rural sewage disposal systems.

A further object of this invention is to provide novel.

compositions of matter comprising biodegradable detergents.

In one aspect an embodiment of this invention resides in a novel biodegradable detergent having the formula:

RCH,CH,

in which M is an alkali metal and R is an alkyl group of from I to about 14 carbon atoms.

A specific embodiment of this invention is found in a biodegradable detergent such as sodium (n-octylcyclohexyl)methano sulfonate.

Other objects and embodiments will be found in the following further detailed description of the present invention.

As hereinbefore set forth, the present inention is concerned with novel compositions of matter and to a process for the preparation of these compounds which are useful as biodegradable detergents, the process being effected in a series of steps. in the first step of the reaction butadiene is reacted with allyl chloride in a Diels- Alder type condensation to give 4-chloromethylcyclohexene. Homologs of butadiene, such as isoprene, or analogous cyclic conjugated dienes such as cyclopentadiene or cyclohexadiene may be used instead of butadiene, and these yield generally similar results, but butadiene is preferred. The Diels-Alder condensation is effected at elevated temperatures usually in the range of from about 50 to about 190 C. and at a pressure ranging from atmospheric up to about atmospheres. The reaction pressure may be attained by the introduction of a substantially inert gas such as nitrogen or argon into the reaction zone, the amount of pressure which is utilized being that which is sufficient to maintain at least a portion of the reactants in the liquid phase.

The 4-chloromethylcyclohexene which is formed according to the above paragraph is then subjected to a hydrogenation step. The chloromethylcyclohexene is selectively hydrogenated in the presence of a noble metal catalyst, these hydrogenation catalysts being well known in the art. Specific examples of these catalysts will include, in particular, platinum and palladium compounds per se or composited on a solid support which is essentially non-acidic in character, examples of these supports being charcoal or kieselguhr. The hydrogenation reaction is effected at hydrogenation conditions which will include a temperature in the range of from about 2S to about 50 C. and at an applied hydrogen pressure which may range from 50 to about 2000 pounds per square inch whereby the chloromethyl substituent remains unchanged, while the cyclohexene ring is hydrogenated to form a cyclohexane ring. Thereafter the chloromethylcyclohexane is then subjected to ring alkylation by reaction with an alphaolefin in the presence of a free-radical generating compound and hydrogen chloride. In an alternative varia tion of this procedure, the hydrogenation of the ring unsaturation may be carried out after the alkylation of the chloromethylcyclohexene, i.e., the hydrogenation may be effected on the resultant n-alkyl-substituted chloromethylcyclohexene.

The chloromethylcyclohexane which has been obtained according to the process set forth in the above paragraph is then selectively alkylated utilizing an olefinic hydrocarbon as the alkylating agent. The selective alkylation in which the alkyl substituent is positioned on the ring rather than on the side chain is effected by treating the reactants in the presence of a free-radical generating compound and hydrogen chloride. in the preferred embodiment of the invention the olefinic hydrocarbon which is utilized as the alkylating agent will comprise an alpha-olefin containing from 3 to about 20 carbon atoms. By utilizing an alkylation catalyst comprising a free-radical generating compound and a promoter comprising hydrogen chloride, it is possible to obtain a normal alkyl side chain on the cyclohexane ring rather than a secondary alkyl side chain which would result if the alkylation were effected in the presence of an acidic catalyst of the Friedel-Crafts type or sulfuric acid, etc. Specific examples of these oleflflle hydrocarbons which are utilized as alkylating agents include l-hexene, l-heptene, l-octene, l-nonene, l-

decene, l-undecene, l-dodecene, l-tridecene, l-tetradecene, etc. It is also contemplated within the scope of this invention that other alpha-olefins containing less than 6 or more than l4 carbon atoms may also be uti' lized, said olefins including propene, l-butene, l-pentene, l-pentadecene, l-hexadecene, l-heptadecene, l-octadecene, l-nonadecene, l-eicosene, etc.

The catalysts which are used in this step of the invention will include peroxy compounds containing the bivalent radical -0 which decompose to form free radicals which initiate the general reaction and are capable of inducing the condensation of the chloromethylcyclohexane with the l-alkene. Examples of these catalysts include the persulfates, perborates, percarbonates of ammonium and of the alkali metals, or organic peroxy compounds. The organic peroxy compounds constitute a preferred class of catalysts for use in the invention and include peracetic acid, persuccinic acid, methyl ethyl ketone peroxide, methyl isobutyl ketone peroxide. acetyl peroxide, dipropionyl peroxide, di-t-butyl peroxide, butyryl peroxide, lauroyl peroxide, benzoyl peroxide, tetralin peroxide, urea peroxide, tbutyl perbenzoate, t-butyl hydroperoxide, methylcyclohexyl hydroperoxide, cumene hydroperoxide, diisopropylbenzene hydroperoxide, etc. Mixtures of peroxy compound catalysts may be employed or the peroxy compound catalyst may be utilized in admixture with various diluents. Thus, organic peroxy compounds which are compounded commercially with various diluents which may be used include benzoyl peroxide compounded with calcium sulfate, benzoyl peroxide compounded with camphor, phthalate esters, etc. Only catalytic amounts (less than stoichiometric amounts) need be used in the process.

The alkylation of the chloromethylcyclohexane with the l-alkene is effected at elevated reaction temperatures which should be at least as high as the initial decomposition temperature of the free-radical generating catalyst, such as the peroxide compound, in order to liberate and form free radicals which promote the reaction. In selecting a particular reaction temperature for use in the process of the present invention, two considerations must be taken into account. First, sufficient energy by means of heat must be supplied to the reaction so that the reactants, namely, the chloromethylcyclohexene and the l-alkenes, will be activated sufficiently for condensation to take place when free radicals are generated by the catalyst. Second, free-radical generating catalysts such as peroxy compounds, particularly organic peroxides, decompose at a measurable rate with time in a logarithmic function dependent upon temperature. This rate of decomposition can be and ordinarily is expressed as the half life of a peroxide at a particular temperature. For example, the half life in hours for di-t-butyl peroxide is l 1 hours at 125 C., 4 hours at 135 C., and 1.5 hours at 145C. A reaction system temperature must then be selected so that the free-radical generating catalyst decomposes smoothly with the generation of free radicals at a half life which is not too long. In other words, sufficient free radicals must be present to induce the present chain reaction to take place, and these radicals must be formed at a temperature at which the reactants are in a suitably activated state for condensation. When the half life of the free-radical generating catalyst in greater than hours, radicals are not generated at a sufficient rate to cause the reaction of the process of the present invention to go forward at a practically useful rate. Thus the 4 reaction temperature may be within the range of from about 50 to about 300 C. and at least as high as the decomposition temperature of the catalyst, by which is meant a temperature such that the half life of the freeradical generating catalyst is not greater than 10 hours. Since the half life for each free-radical generating catalyst is different at different temperatures, the exact temperature to be utilized in a particular reaction will vary. However, persons skilled in the art are well acquainted with the half life vs. temperature data for different free-radical generating catalysts. Thus it is within the skill of one familiar with the art to select the particular temperature needed for any particular catalyst. However, the operating temperatures generally do not exceed the decomposition temperature of the catalyst by more than about C. since free-radical generating catalysts decompose rapidly under such conditions. For example, when a free-radical generating catalyst such as t-butyl perbenzoate is used, having a 50% decomposition temperature (in 10 hours) of approximately l05 C., the operating temperature of the process is from about to about 205 C. When di-tbutyl peroxide having a 10 hour, 50% decomposition temperature of about C. is used, the process is run at a temperature ranging from about 125 to about 225 C. Higher reaction temperatures may be employed, but little advantage is gained if the temperature is more than the hereinbefore mentioned 100 C. higher than the 10 hour, 50% decompsoition temperature of the catalyst. The general effect of increasing the operating temperature is to accelerate the rate of condensation reaction of the chloromethylcyclohexane with the lalkene. However, the increased rate of reaction is accompanied by certain amounts of decomposition. in addition to the elevated temperatures which are utilized, the reaction may also be effected at elevated pressures ranging from about I to about 100 atmospheres or more, the preferred operating pressure of the process being that which is required to maintain a substantial portion of the reactants in liquid phase. Pressure is not an important variable in the process of this invention. However, because of the low boiling points of some of the reactants it is necessary to utilize pressure-withstanding equipment to insure liquid phase conditions. In batch type operations, it is often desirable to utilize pressure-withstanding equipment to charge the reactants and the catalyst to the vessel and to pressure the vessel with 10 or 30 or 50 or more atmospheres of an inert gas such as nitrogen. This helps to insure the presence of liquid phase conditions. However, when the mole quantity of reactants is sufficient, the pressure which they themselves generate at the temperature utilized is sufficient to maintain the desired phase conditions.

Furthermore, the concentration of the catalyst employed in this process may vary over a rather wide range but it is desirable to utilize low concentrations of catalysts such as from about 0.1% to about 10% of the total weight of the combined starting materials charged to the process. The reaction time may be within the range of from less than 1 minute to several hours, depending upon temperature and the half life of the catalyst. Generally speaking, contact times of at least l0 minutes are preferred.

In addition to the free-radical generating catalyst, the alkylation is also effected in the presence of a hydrogen chloride compound. The hydrogen chloride compound is used as a promoter for the reaction and also is used to prevent or inhibit telomerization, said telomerization being a polymerization reaction in which unwanted side reaction products may be formed. The hydrogen chloride may be present as anhydrous hydrogen chloride, as concentrated hydrochloric acid or as an aqueous solution of hydrochloric acid, the hydrochloric acid being present in an amount of from 5 to about 38% in said aqueous solution.

The resulting disubstituted cyclohexane comprising an n-alkyl-substituted chloromethylcyclohexane is thereafter reacted with an alkali metal salt of a sulfurcontaining compound such as an alkali sulfite or alkali bisulfite to obtain the desired product. Representative examples of these alkali metal salts include sodium sulfite, sodium bisulfite, potassium sulfite, potassium bisulfite, lithium sulfite, lithium bisulfite, rubidium sulfite, rubidium bisulfite, cesium sulfite, cesium bisulfite, etc., the preferred compounds comprising the sodium or potassium salts due to their relatively lower cost and greater availability. The reaction is usually effected at elevated temperatures in the range of from about 50 to about 150 C. or more and at atmospheric pressure. Preferably the sulfonation is effected in the presence of a highly polar or highdielectric solvent, said solvents including dimethyl sulfoxide, dimethylformamide, sulfolane, dioxane, ethanol, ethylene glycol, glycerol, nitromethane, etc.

The process of this invention in which the novel compositions of matter useful as biodegradable detergents ate prepared may be effected in either a batch type or continuous type of operation. When a batch type operation is used, a quantity of the allyl chloride is placed in an appropriate apparatus such as an autoclave and butadiene is charged thereto. The autoclave is then heated to the desired operating temperature and pressure in the range hereinbefore set forth and maintained thereat for a predetermined residence time which may range from about 0.5 up to about hours or more in duration. Upon completion of the desired residence time, heating is discontinued, the autoclave is allowed to return to room temperature, the excess pressure is vented and the reaction mixture is recovered. The 4- chloromethylcyclohexene is separated from any unreacted allyl chloride by conventional means such as distillation or any other separation means known in the art and placed in a second reaction vessel wherein the chloromethylcyclohexene is selectively hydrogenated by passage over a catalyst such as a platinumor pal ladium-containing compound in the presence of a hydrogen stream at a temperature and pressure within the range hereinbefore set forth, the cyclohexene ring being selectively and relatively completely hydrogenated to form a cyclohexane ring.

The chloromethylcyclohexane is then placed in another reaction vessel along with a free-radical generating compound and the l-alkene which is to be utilized as the alkylating agent, said alkylating vessel preferably comprising an autoclave of the rotating or mixing type. In addition, a promoter comprising hydrogen chloride either in gaseous form as hydrogen chloride or in aqueous form as hydrochloric acid is added to the reactor which is thereafter heated to the desired operating tem perature which, as hereinabefore set forth, is at least as high as the decomposition temperature of said freeradical generating compound. After maintaining the alkylation reaction at this temperature for a predetermined period of time, heating is discontinued, the reaction mixture is allowed to return to room temperature and the alkyl-substituted chloromethylcyclohexane is recovered by conventional means. The n-alkyl chloromethylcyclohexane is reacted with the alkali metal salt of a sulfur-containing compound at elevated temperatures and in the presence of a solvent of the type hereinbefore set forth. Following the sulfonation step which may take again from about 0.5 up to about 10 hours or more, heating is discontinued and the desired product is separated from the solvent by fractionation and passed to storage.

It is also contemplated within the scope of this invention that the desired product may be prepared while employing a continuous type of operation. When the continuous type of operation is to be used, the starting materials comprising the allyl chloride and butadiene are continuously charged to a reactor which is maintained at the proper operating conditions of temperature and pressure. After passage thrugh this reactor, the effluent is continuously withdrawn, subjected to a separation step whereby the unreacted allyl chloride and butadiene are separated from the chloromethylcyclohexene and recycled to form a portion of the feed stock while the latter is continuously charged to a hydrogenation apparatus along with a stream of hydrogen sufficient to maintain the desired operating pressure. The hydrogen aand 4-chloromethylcyclohexene are continuously passed over a hydrogenation catalyst of the type hereinbefore set forth at a temperature in the range of from about 25 to about 50 C. and the resulting product is continuously withdrawn. The product which has been selectively and usually relatively completely hydrogenated to form chloromethylcyclohexane is thereafter charged to an alkylation apparatus which is also maintained at the proper operating conditions of temperature and pressure. In addition, the lalkene, the free-radical generating compound and the hydrogen chloride promoter are also continuously charged to this alkylation apparatus through separate lines. After completing the desired residence time in the alkylation apparatus, the reactor effluent is continuously withdrawn and again subjected to separation steps whereby unreacted starting materials, promoter, free-radical generating compound and by-products are separated from the alkyl-substituted chloromethylcyclohexane. The unreactedmaterials are recycled to form a portion of the feed stock to the apparatus while the alkyl-substituted chloromethylcyclohexane is continuously charged to a sulfonation reactor. The alkali metal sulfur-containing compound such as sodium bisulfite, etc., is continuously charged to the sulfonation reactor along with the solvent. The solvent may be charged to the reactor through a separate line or one or both of the reactants may be admixed with the solvent prior to entry into said reactor and the resulting mixture charged thereto in a single stream. After completion of the desired residence time in the sulfonation reactor, the effluent is again continuously withdrawn and subjected to separation steps which are conventional in nature whereby unreacted starting material and solvent are separated from the desired compound, the latter being passed to storage while the unreacted starting materials are recycled to form a portion of the feed stock.

Some specific examples of the novel compositions of matter which may be prepared according to the process hereinbefore set forth will include those compounds having the generic formula:

RCH C in which M is an alkali metal and R is an alkyl group of from 1 to about l4 carbon atoms such as sodium(npropylcyclohexyDmethano sulfonate, potassium(n propylcyclohexyl)methano sulfonate, lithium(npropylcyclohexy)methano sulfonate, cesium(n-propylcyclohexyl)methano sulfonate, sodium(n-butylcyclohexyl)methano sulfonate, potassium(n-butylcyclohexyl)methano sulfonate, lithium(n-butylcyclohexyl)methano sulfonate, cesium(n-butylcyclohexyl)methano sulfonate, sodium(n-pentylcyclohexyl)methano sulfonate, potassium(n-pentylcyclohexyl)methano sulfonate, lithium(n-pentylcyclohexyl)methano sulfonate, cesium(n-pentylcyclohexyl)methano sulfonate, sodium(n-hexylcyclohexyl)methano sulfonate, potassium(n-hexylcyclohexyl)methano sulfonate lithium(nhexylcyclohexyl)methano sulfonate, cesium(n-hexylcyclohexyl)methano sulfonate, sodium(n-heptylcyclohexyl)methano sulfonate, potassium(n-heptylcyclohexyl)methano sulfonate, lithium(n-heptylcyclohexyl)methano sulfonate, cesium(n-heptylcyclohexyllmethano sulfonate, sodium(n-octylcyclohexyl)methano sulfonate, potassium(n-octylcyclohexyl)methano sulfonate, lithium(n-octylcyclohexyl)methano sulfonate, cesium(n-octylcyclohexyl)methano sulfonate, sodium(n-nonylcyclhexyl)methano sulfonate, potassium(n-nonylcyclohexy)methano sulfonate, lithium(n-nonylcyclohexyl)methano sulfonate, cesium(nnonylcyclohexyl)methano sulfonate, sodium(n-decylcyclohexyl)-methano sulfonate, potassium(n-decylcyclohexyl)methano sulfonate, lithium(n-decylcyclohexyl)methano sulfonate, cesiumtn-decylcyclohexyl)methano sulfonate, sodium(n-undecylcyclohexyl)methano sulfonate, potassium(n-undecylcyclohexyUmethano sulfonate, lithium(n-undecylcyclohexyDmethano sulfonate, cesium(n-undecylcyclohexyl)methano sulfonate, sodium(n-dodecylcyclohexyl)methano sulfonate, potassium(n-dodecylcyclohexyl)methano sulfonate, lithium(n-dodecylcyclohexyl)methano sulfonate, cesium(n-dodecylcyclohexyl)methano sulfonate, sodium(n-tetradecylcyclohexyl)methano sulfonate,

potassium(n-tetradecylcyclohexyl)methano sulfonate, lithium(n-tetradecylcyclohexyl)methano sulfonate, cesium(n-tetradecylcyclohexyl)methano sulfonate,

etc. It is to be understood that the aforementioned biodegradable detergents are only representative of the novel class of compounds, and that the present invention is not necessarily limited thereto.

The following examples are given to illustrate the novel compounds of the present invention and the process for the preparation thereof; however, these examplles are not intended to limit the generally broad scope of the present invention in strict accordance therewith.

EXAMPLE I In this example 76.5 grams (1.0 mole) of allyl chloride is placed in the glass liner of a rotating autoclave. The liner is sealed into the autoclave and 54 grams l .0 mole) of butadine is charged thereto. The autoclave is heated to a temperature of C. and maintained thereat for a period of 4 hours. At the end of this time, heating is discontinued and the autoclave is allowed to return to room temperature. The autoclave is opened and the reaction mixture is recovered therefrom. This mixture is then subjected to fractional distillation whereby the 4-chloromethylcyclohexene is separated from any unreacted allyl chloride and recovered.

The thus prepared chloromethylcyclohexane is charged to a reactor which is loaded with a catalyst comprising platinum composition on granular charcoal, said charge being effected at a temperature which is maintained below 50 C. The chloromethylcyclohexene is charged to the reactor at a liquid hourly spaced velocity of 0.5 along with a stream of hydrogen in an amount sufficient to maintain a hydrogen pressure of 1000 pounds per square inch. After passage over the catalyst, the effluent stream is withdrawn to a separation zone whereby the hydrogen gas is separated from the organic liquid phase. Bromine number determinations on the product show that approximately 95% comprises the desired product, chloromethylcyclohexane.

The chloromethylcyclohexane which is prepared according to the above paragraph is then placed in the glass liner of a rotating autoclave along with l-octene, a catalyst comprising di-t-butyl peroxide and concentrated hydrochloric acid, the chloromethylcyclohexane being in a molar excess over the l-octene. The autoclave is sealed and nitrogen is pressed in until an initial operating pressure of 30 atmospheres is reached, after which the autoclave is heated to a temperature of I30 C. The autoclave is maintained at a temperature in the range of from about to C. for a period of 8 hours, following which heating is discontinued, the autoclave is allowed to return to room temperature and the excess pressure is discharged therefrom. The autoclave is opened, the reaction product is recovered and subjected to conventional means of separation whereby the n-octyl-substituted chloromethylcyclohexane is separated and recovered.

The n-octyl-substituted chloromethylcyclohexane is then treated in a manner similar to that hereinbefore set forth with sodium sulfite at a temperature of about 60 C. in the presence of a solvent comprising dimethyl sulfoxide, for a period of 4 hours. At the end of this time, heating is discontinued, the mixture is recovered and subjected to conventional means of separation whereby the desired product comprising sodium(noctylcyclohexyl)methano sulfonate is separated and recovered.

EXAMPLE ll In this example 4-chloromethylcyclohexene is prepared in a manner similar to that hereinbefore set forth. The thus prepared 4-chloromethylcyclohexene which results from the condensation in a Diels-Alder manner between butadiene and allyl chloride is then charged to a reactor which has been loaded with a hydrogenation catalyst comprising palladium composited on kieselguhr. The 4-chloromethylcyclohexene is charged to the reactor at a temperature of about 40 C., a liquid hourly space velocity of 05 along with a stream of hydrogen sufficient to maintain a hydrogen pressure of 2000 pounds per square inch. After passage over the catalyst, the effluent stream is withdrawn to a separation zone whereby the hydrogen gas is separated from the liquid phase. This liquid phase is found to comprise 9 over 90% of the desired product, chloromethylcyclohexane.

The aforementioned chloromethylcyclohexane along with l-tetradecene, benzoyl peroxide and concentrated hydrochloric acid are placed in an alkylation apparatus and heated to reflux at a temperature in the range of from about 80 to 85 C. for a period of 4 hours. At the end of the 4-hour period, heating is discontinued and the reactor is allowed to return to room temperature. The reaction mixture is recovered, subjected to distillation whereby the desired product comprising n-tetradecyl-substituted chloromethylcyclohexane is recovered. The n-tetradecyl-substituted chloromethylcyclohexane is then reacted with sodium sulfite at a temperature of about 75 C. for a period of 4 hours in the presence of a solvent comprising l,4-dioxane. At the end of the 4- hour period, heating is discontinued, and the reaction mixture is allowed to cool to room temperature. After cooling to room temperature, the mixture is subjected to conventional means of separation whereby the desired product comprising sodium(n-tetradecylcyclohexyl)methano sulfonate is recovered.

EXAMPLE III in a manner similar to that set forth in Example I above, allyl chloride is reacted with butadiene in equimolar proportions to form 4-chloromethylcyclohexene. This compound is then charged to a reactor which contains a hydrogenation catalyst comprising platinum composited on charcoal. After charging the 4- chloromethylcyclohexene to the reactor at a temperature of about 40 C. and a liquid hourly space velocity of 0.5 along with a stream of hydrogen which is sufficient to maintain a hydrogen pressure of 2500 pounds per square inch, the effluent stream is withdrawn to a separation zone and the hydrogen gas is separated from the liquid phase.

A molar excess of the chloromethylcyclohexane, loctene, t-butyl peroxide and concentrated hydrochloric acid are placed in an alkylation apparatus and heated to reflux at a temperature in the range of from I30 to 140 C. for a period of 4 hours. Thereafter the heating is discontinued and the reactor is allowed to return to room temperature. The reaction mixture is recovered and subjected to fractional distillation whereby the desired product comprising n-octyl-substituted chloromethylcyclohexane is recoverd. This compound is then reacted with potassium bisulfite at a temperature of about 75 C. for a period of 4 hours in the presence of adimethyl sulfoxide solvent. At the end of the 4-hour period, heating is discontinued, the reaction mixture is allowed to cool to room temperature and thereafter is subjected to conventional means of separation whereby the desired product comprising potassium(n-octylcyclohexy)methano sulfonate is recovered.

EXAMPLE IV In a manner similar to that set forth in the above examples, 4-chloromethylcyclohexene which is prepared by the reaction of equimolar quantities of allyl chloride and butadiene at a temperature of [25 C. is selectively hydrogenated by passage over a hydrogenation catalyst comprising platinum composited on kieselguhr, the hydrogenation conditions including a temperature of about 40 C., a liquid hourly space velocity of 0.5 and an applied hydrogen pressure of 2000 pounds per sqaure inch. The desired product comprising chloromethylcyclohexane is separated from the hydrogen gas and alkylated by being placed in a glass liner of a rotating autoclave along with l-dodecene, di-t-butyl peroxide and hydrochloric acid, said chlormethylcyclohexane being present in a molar excess. After alkylating at conditions which include a temperature in the range of from to C. and a pressure of 30 atmospheres of nitrogen for a period of 4 hours, heating is discontinuted, the autoclave is allowed to return to room temperature and the excess pressure is discharged. The autoclave is opened and the reaction mixture which is recovered therefrom is subjected to fractional distillation under reduced pressure to separate and recover n-dodecyl-substituted cyclohexylmethyl chloride.

The aforementioned compound is sulfonated by treating the compound with an equimolar amount of potassium sulfite in the presence of a dimethylsulfoxide solvent, said reaction being effected at a temperature of 50 C. for a period of 4 hours. At the end of the aforementioned 4-hour period, heating is discontinuted and upon cooling the reaction mixture is separated from the solvent and any unreacted starting materials, the desired product comprising potassium(n-dodecylcyclohexyhmethano sulfonate being recovered therefrom.

EXAMPLE V In the glass liner of a rotating autoclave is placed 76.5 grams (1.0 mole) of allyl chloride after which the liner is sealed and 54 grams (1.0 mole) of butadiene is charged thereto. Following this, the autoclave is then heated to a temperature of 125 C. and maintained thereat for a period of 4 hours. At the end of the 4-hour period, heating is discontinued and the autoclave is allowed to return to room temperature. The autoclave is opened, the reaction mixture is recovered therefrom and subjected to fractional distillation under reduced pressure whereby the desired product comprising 4- chloromethylcyclohexene is separated from any unreacted allyl chloride and recovered.

The 4-chloromethylcyclohexene is then charged to a reactor which is loaded with a catalyst comprising platinum composited on granular charcoal, said charge being effected at a temperature which is maintained below 50 C. The aforementioned chloromethylcyclohexane is hydrogenated under conditions which include a liquid hourly spaced velocity of 0.5 and a hydrogen charge sufficient to maintain a pressure of 2000 pounds per square inch. After passage over the catalyst, the effluent stream is withdrawn to a separation zone whereby the hydrogen gas is separated from the organic liquid phase. Thereafter the chloromethylcyclohexane is placed in the glass liner of a rotating autoclave along with l-hexadecene, the charge stock consisting of a molar excess of the chloromethylcyclohexane over the l-hexadecene in a range of from about 1.5:] to about 2:1 moles of chloromethylcyclohexane per mole of l-hexadecene. In addition to the reactants, 7 grams of di-t-butyl peroxide and 20 grams of concentrated hydrochloric acid are also placed in the autoclave. Thereafter the autoclave is sealed and nitrogen is pressed in until an initial operating pressure of 30 atmospheres is reached. The autoclave and contents thereof are then heated to a temperature of about 1 30 C. and maintained in a range of from 130 to 140 C. for a period of 8 hours. At the end of the 8-hour period, heating is discontinued, the autoclave is allowed to return to room temperature and the excess pressure is discharged therefrom. The autoclave is opened, the reaction mixture is recovered and subjected to fractional distillation under reduced pressure whereby the desired product comprising n-hexadecyl-substituted cyclohexylmethyl chloride is recovered.

The n-hexadecyl-substituted cyclohexylmethyl chloride which is prepared according to the above paragraph is then sulfonated by placing said compound in a flask along with an equimolar amount of sodium sulfite and a solvent comprising dioxane. The flask is then heated to a temperature of about 50 C. and maintained thereat for a period of 4 hours, at the end of which time heating is discontinuted. Upon cooling, the reaction mixture is separated from the solvent and any unreacted starting material by conventional means, the desired product comprising sodium(n-hexadecylcyclohexyl)methano sulfonate being recovered therefrom.

I claim as my invention:

l. A novel biodegradable detergent having the formula:

RCHs H: 

1. A NOVEL BIODEGRADABLE DETERGET HAVING THE FORMULA:
 2. The novel biodegradable detergent as set forth in claim 1 being sodium(n-octylcyclohexyl)methano sulfonate.
 3. The novel biodegradable detergent as set forth in claim 1 being potassium(n-octylcyclohexyl)methano sulfonate.
 4. The novel biodegradable detergent as set forth in claim 1 being potassium(n-dodecylcyclohexyl)methano sulfonate.
 5. The novel biodegradable detergent as set forth in claim 1 being sodium(n-tetradecylcyclohexyl)methano sulfonate.
 6. The novel biodegradable detergent as set forth in claim 1 being sodium(n-hexadecylcyclohexyl)methano sulfonate 